| 摘要 |
<p>Producing kerosene and diesel fuel and co-production of hydrogen from a light saturated charge (F1) having (a) light naphtha cut (NL), and (b) 3C/4C (LPG) cut, comprises: dehydrogenation (2) of the charge using a dehydrogenation catalyst having e.g. a noble metal group VIII e.g. platinum, to obtain olefinic effluent (F2); oligomerization (3) of all/part of the effluent in an oligomerization unit using oligomerization catalyst e.g. ion exchange resins, to obtain an effluent (F4); and entirely/partly hydrogenating (4) the effluent (F3) in liquid phase in one or more fixed bed reactors. Producing kerosene and diesel fuel and co-production of hydrogen from light saturated charge (F1) of a carbon number of 3-7C comprising (a) light naphtha cut (NL) having number of carbon atoms of 5-7 obtained from primary distillation units, hydrocracking unit or Fischer Tropsch unit, from interval of distillation of 30-120[deg] C, where the light naphtha cut is previously hydrotreated to be freed from oxygen nitrogen and sulfur compound, and (b) 3C/4C (LPG) cut in any proportion, freed from oxygenated and sulfur compound, comprises: dehydrogenation (2) of the charge operating at pressure of 1.3-5 absolute bars and at a temperature of 400-700[deg] C, preferably 500-600[deg] C, using a dehydrogenation catalyst consisting of a noble metal group VIII comprising platinum, iridium or rhodium, and at least one promoter comprising tin, germanium, lead, gallium, indium, and thallium, where the noble metal and the promoter is deposited on an inert support comprising silica, alumina, titania oxide, and/or magnesia silica and the dehydrogenation step to recover an effluent (F2) mainly comprises olefins having number of carbon atoms of 3-7, called olefinic effluent (F2); oligomerization (3) of all or part of the obtained olefin effluent (F2) in an oligomerization unit using oligomerization catalyst comprising solid phosphoric acid, ion exchange resins, alumina silica or silico aluminates such as pure zeolites or supported on alumina, where the oligomerization for recovering an effluent (F3) mainly comprises olefins of 10-25C, and an effluent essence (F4) mainly comprises paraffins of 5-10C which is separated from the effluent (F3) by distillation and recycled at the inlet of the oligomerization unit; and entirely or partly hydrogenating (4) the obtained olefinic effluent (F3) carried out in liquid phase in one or more fixed bed reactors, at temperatures of 50-350[deg] C, preferably 100-200[deg] C and under pressures of 5-50 bars, preferably 10-30 bars, and using a hydrogenation catalyst containing a metal comprising platinum, palladium or nickel, deposited on an inert support such as silica and/or alumina, where the hydrogenation step for recovering an effluent (F6) is a kerosene or diesel cut mainly paraffinic.</p> |
